WO1999022127A1 - Systeme de production industrielle d'energie a rendement eleve, non polluant et de technologie de pointe - Google Patents

Systeme de production industrielle d'energie a rendement eleve, non polluant et de technologie de pointe Download PDF

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Publication number
WO1999022127A1
WO1999022127A1 PCT/US1998/022763 US9822763W WO9922127A1 WO 1999022127 A1 WO1999022127 A1 WO 1999022127A1 US 9822763 W US9822763 W US 9822763W WO 9922127 A1 WO9922127 A1 WO 9922127A1
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WO
WIPO (PCT)
Prior art keywords
combustion chamber
turbine stage
mixture
gas generator
reheater
Prior art date
Application number
PCT/US1998/022763
Other languages
English (en)
Inventor
Rudi Beichel
Original Assignee
Rudi Beichel
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Rudi Beichel filed Critical Rudi Beichel
Priority to AU12023/99A priority Critical patent/AU1202399A/en
Priority to EP98955147A priority patent/EP1029167A1/fr
Priority to CA002306710A priority patent/CA2306710A1/fr
Priority to JP2000518198A priority patent/JP2003526035A/ja
Publication of WO1999022127A1 publication Critical patent/WO1999022127A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04636—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a hybrid air separation unit, e.g. combined process by cryogenic separation and non-cryogenic separation techniques
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K21/00—Steam engine plants not otherwise provided for
    • F01K21/04—Steam engine plants not otherwise provided for using mixtures of steam and gas; Plants generating or heating steam by bringing water or steam into direct contact with hot gas
    • F01K21/047—Steam engine plants not otherwise provided for using mixtures of steam and gas; Plants generating or heating steam by bringing water or steam into direct contact with hot gas having at least one combustion gas turbine
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
    • F02C3/22—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being gaseous at standard temperature and pressure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
    • F02C3/30—Adding water, steam or other fluids for influencing combustion, e.g. to obtain cleaner exhaust gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/34—Gas-turbine plants characterised by the use of combustion products as the working fluid with recycling of part of the working fluid, i.e. semi-closed cycles with combustion products in the closed part of the cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04533—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the direct combustion of fuels in a power plant, so-called "oxyfuel combustion"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/80—Processes or apparatus using other separation and/or other processing means using membrane, i.e. including a permeation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • Smog Air pollution, commonly called "smog" is a very serious problem in most major metropolitan cities. Smog includes sulfur dioxides and nitrous oxides which form a brown cloud in the surrounding air. While much of the smog comes from automobiles, trucks, and busses, other sources of smog include the power generation industry, for example, which burns coal, natural gas and/or oil to produce electrical power.
  • the hot air produced by the flame was flowed over a series of pipes, through which flowed water, to produce steam.
  • Overall efficiencies for producing electricity were very low (approximately 10% of the lower heating value of the fuel), and the pollution of the surrounding environment was very high. In those days, the pollution was caused by the smoke and haze generated by the combustion process, and the carbon dust deposited out of the smoky exhaust.
  • Combined cycle systems use a gas turbine much like that used in an airplane to drive the primary power generator.
  • a series of axial flow compressor stages boosts the pressure of the incoming air up to combustion pressure in the gas generator where it is mixed with fuel -and ignited.
  • the hot gases are then exhausted into a series of turbine stages where the heat energy is turned to work in terms of shaft horsepower.
  • the shaft horse power is then turned into electrical power in the generator.
  • the conventional industrial power generation systems are relatively large, often generating hundreds of megawatts or even gigawatts of power and occupying many acres of land.
  • An inadvertent shut down, for example, of an industrial power generation system may impact the quality of electricity supplied to consumers if the other generating systems in the electricity network -are not equipped to compensate for the shut down.
  • these industrial power generation systems are too large for a smaller consumer (such as a train or ship) to have their own systems. Therefore, individual business, schools, and residential communities are typically forced to rely on outside sources of electricity. These outside sources have complex distribution systems in which much power is lost in the transmission to the consumer. Furthermore, the consumer may be forced to pay unreasonably high prices for electrical power from an outside source.
  • a low pollution industrial power generation system has a source of fuel .and source of oxygen rich gas having less nitrogen (e.g., no nitrogen) than is present in air and more oxygen than is present in air.
  • a mixing unit is configured to receive and mix at least the oxygen rich gas and the fuel to form a mixture.
  • the oxygen rich gas is mixed with steam prior to being mixed with the fuel.
  • a combustion chamber is in selective fluid communication with the mixing unit through a valve. Within the combustion chamber, an igniter is configured to ignite the mixture downstream of the injector face. In one embodiment, the system is closed loop and emits no pollution.
  • a low pollution industrial power generation method includes providing a source of fuel and source of oxygen rich gas having less nitrogen than is present in air and more oxygen than is present in air.
  • a mixing unit receives .and mixes at least the oxygen rich gas and the fuel to form a mixture.
  • Combustion ch-amber walls define a combustion chamber which receives the mixed fuel .and oxygen rich gas from the mixing unit.
  • An igniter within the combustion chamber ignites the mixture downstream of the injector face.
  • steam a heat absorbing medium
  • oxygen rich gases e.g., substantially pure oxygen
  • fuel e.g., methane
  • Combustion chamber pressure is on the order of approximately 3300 PSIA.
  • the essentially inert nitrogen (78% of the air by volume) of the air is a heat absorbing medium which absorbs a large portion of the combustion generated heat. This nitrogen thus lowers the combustion temperature compared to the combustion temperature if no heat absorbing medium was used.
  • the industrial power generation system of the present invention reduces or eliminates the amount of nitrogen used as a heat absorbing agent. Instead, a heat absorbing agent other than nitrogen such as H 2 O is used to reduce nitrous oxide emissions.
  • water is added to the combustion process.
  • the water in the fuel/oxygen mixture is a more efficient heat absorbing medium than is nitrogen in the fuel/air mixture because water can absorb more heat per unit mass.
  • the exemplary embodiment reduces or eliminates nitrous oxide emissions and provides an efficient way to absorb combustion heat.
  • the mixing of the fuel and oxygen prior to entering the combustion chamber promotes efficient combustion thereby improving the combustion efficiency of the power generation system.
  • An industrial gas generator comprises a source of heat absorbing agent in a liquid phase (e.g., in one embodiment, a water reservoir although other liquids can also be used if appropriate).
  • Combustion chamber walls define a combustion chamber and define channels which fluidly connect the reservoir with the combustion chamber and thus allow water to pass from the reservoir to the combustion chamber.
  • the liquid phase heat absorbing agent e.g., water
  • the heat absorbing agent evaporates before entering the combustion chamber, thereby cooling the combustion chamber walls.
  • An industrial gas generation method includes providing the heat absorbing agent in a liquid phase, and passing the heat absorbing agent through the combustion chamber walls to the combustion chamber thereby cooling the combustion chamber walls.
  • the heat absorbing agent in a liquid phase passes through channels defined in a combustion chamber wall and into a combustion chamber, wherein the heat absorbing agent changes from a liquid phase to a gaseous phase as the heat absorbing agent passes through the plurality of channels and thereby cools the combustion chamber walls.
  • This type of cooling is called transpiration cooling.
  • Water is very effective for this purpose since use is made of the latent heat of water as well as its sensible heat.
  • Latent heat is the heat required (usually measured in BTU/ pound of H 2 O) to evaporate and/or condense water and/or steam at saturation conditions. For water, this amounts to 900-1000 BTU/pound of H 2 O. It takes a temperature change of approximately 1900°F in sensible heat content of H 2 O in order to provide an equivalent heat change. Therefore, the present invention permits the combustion temperature within a power generation system to be even higher than the melting point of the material of the combustion chamber walls because these walls are cooled to below the melting point temperature if an adequate flow of water is provided through the openings in these walls into the combustion chamber.
  • a low pollution industrial power generation system includes a gas generator.
  • the gas generator includes a combustion chamber portion which is configured to generate mainstream gases.
  • a primary turbine stage is downstream of the combustion chamber, a reheater is downstream of the primary turbine stage, a secondary turbine stage is downstream of the reheater, and a heat exchanger is downstream of the secondary turbine stage.
  • the heat exchanger is configured to tr.ansfer heat from the mainstream gases to an auxiliary fluid flow.
  • An auxiliary turbine stage is configured to receive the auxiliary fluid flow and generate additional electricity from the auxiliary fluid.
  • an industrial power generation method includes combusting oxygen rich gases in a combustion chamber to form mainstream gases, expanding the mainstream gases from the combustion chamber through a primary turbine stage, reheating the mainstream gases from the primary turbine stage, expanding the mainstream gases from the reheater through a secondary turbine stage, transferring heat from the mainstream gases from the secondary turbine stage to an auxili.ary flow, and expanding the auxiliary flow in an auxiliary turbine stage.
  • Each stage generates electricity thereby increasing the efficiency of the overall power generating system relative to the prior art.
  • Turbines transform heat into mechanical energy to drive an electrical generator. With each turbine stage the gas temperature drops as the heat content is incrementally reduced, thereby reducing the energy derived from each subsequent stage. Installing reheaters between stages permits an increase in gas energy content such that the subsequent stage or stages are capable of yielding more overall electrical power.
  • the reheat is accomplished by adding a small amount of fuel to the oxygen rich mainstream gases. Since the gas ignition temperature is less than the actual gas temperature in the reheater, combustion takes place spontaneously without an external ignition source. Since the pressure ratio across each series of turbine stages is essentially constant, the potential power delivered by each stage is essentially the same when the inlet temperatures are identical. In contrast, without reheat stages, the energy delivered by each stage continually decreases resulting in a lower overall cycle efficiency.
  • Auxiliary steam power generation converts, into electricity, most of the heat remaining in the mainstream gases after most of the pressure has been used by the primary and secondary turbine stages.
  • the mainstream gases are brought back to essentially ambient conditions through heat transfer to steam in a steam power generation system.
  • the use of the heat and pressure of the mainstream gases increases the overall efficiency of the power generation system.
  • the power necessary to drive all the pumps is negligible comp.ared to the total system output power.
  • the invention allows systems to be build with a wide range of power outputs.
  • a typical system in accordance with this invention could produce a total power output of, for example, 12.56 megawatts using a pump power of only about 195 kilowatts resulting in a net power output of, for example 12.36 megawatts.
  • Fig. 1 shows schematically the overall industrial power generation system showing how each of the individual systems is related in accordance with the present invention.
  • Fig. 2 shows schematically the oxygen production system of Fig. 1.
  • Fig. 3 shows schematically the gas generator of Fig. 1 with subsequent gas treatment systems prior to the gas entering the gas turbines.
  • Fig. 4 shows schematically the radial and axial turbines used in the main power system of Fig. 1 to produce the electrical power and shows the interstage reheat systems.
  • Fig. 5 shows schematically the auxiliary steam power system of Fig. 1 that recovers waste heat from the main power system.
  • Fig. 6 A shows an exploded isometric view of two flat ring-shaped platelets which are part of the series of platelets shown in Fig. 3 used to transpiration cool the combustion chamber.
  • Fig. 6B shows a detailed exploded isometric view of a portion of Fig. 6A showing channels within the platelets.
  • Fig. 7 shows an isometric view of an embodiment of a reheater used in accordance with the principles of the present invention.
  • Fig. 8 A shows an exploded view of a platelet heat exchanger used in accordance with the principles of the present invention.
  • Fig. 8B shows the platelet heat exchanger of Fig. 8 A in an unexploded view.
  • Beichel patent which is incorporated herein by reference in its entirety.
  • high pressure liquid oxygen and fuel are separately delivered to a gas generator combustion chamber for combustion. After combustion, the mainstream gases pass through turbines where the thermal energy drives electrical generators.
  • the present invention uses the oxygen present in oxygen rich gas, not air, to burn the fuel (e.g., fossil fuel or a fuel including compounds containing carbon and hydrogen, at least one of the compounds in the fuel including the element carbon).
  • the oxygen rich gas contains less nitrogen (e.g., the nitrogen has a mole percentage of 10% or less, 1% or less, or even 0%) than is present in air and more oxygen (e.g., the oxygen has a mole percentage of 50% or more, 99% or less, or even 99% or more) than is present in air.
  • the lower the nitrogen content of the oxygen the lower the nitrous oxide emissions.
  • the oxygen rich gas and the fuel are mixed prior to entering a combustion chamber where the mixture is ignited and burned.
  • the oxygen is mixed with the fuel at higher than stoichiometric conditions such that there is slightly more oxygen than necessary to completely combust all of the fuel.
  • the exemplary embodiment is an industrial power generation system emitting substantially zero pollution, having high efficiency (e.g., 70% or above), and generating net power of approximately 12.36 megawatts.
  • the exemplary embodiment is an example only.
  • the overall system is made up of four subsystems, the oxygen production system, the gas generation system, the main power system, and the auxiliary power system. Each subsystem contributes in its own way toward making the power generation system of the present invention a substantial improvement over the prior art with respect to efficiency and pollution.
  • Fig. 1 is a schematic drawing showing the overall industrial power generation system 1 and the processes implemented in the system 1.
  • Fig. 2 shows the oxygen production system 20 ("source of oxygen rich gas 20") which is one part of the overall power generation system 1 shown in Fig. 1.
  • the oxygen production system 20 converts air into high pressure gaseous oxygen. In the exemplary embodiment in which 12.56 megawatts of power is produced, oxygen production system 20 produces oxygen at 3.4 pounds per second ("lbm/s").
  • air from, for example, the ambient environment is initially dried and cleansed by passing through filter/drier 101.
  • Filter/drier 101 may be a two stage system having a drier portion and a filter portion.
  • the drier portion may include silica gel which absorbs most of the moisture (H 2 O) in the air.
  • the filter portion removes particulates from the air.
  • filter/drier 101 may contain a redundant parallel filter/drier 101a to allow the oxygen production system 20 to operate when servicing filter/drier 101 or to increase air intake capacity.
  • a low pressure compressor 102 receives and compresses the clean air to, for example, 25 to 40 PSIA.
  • a continuous membrane column 103 receives the compressed air and filters out most of the nitrogen (N 2 ). Argon, oxygen, H 2 O, .and CO 2 and only about 20% N 2 .are allowed to pass to the outlet 104 of the continuous membrane column 103.
  • Continuous membrane columns are commonly available on the market and are effective in extracting oxygen rich gases from air.
  • the left quadrants 103i and 103ii and the right quadrants 103iii and 103iv of the continuous membrane column 103 are separated by a membrane 103a comprising capillary or hollow fiber membranes.
  • the flow is generally downward from the upper left quadrant 103i to the lower left quadrant 103ii and generally upward from the lower right quadrant 103iii to the upper right quadrant 103iv.
  • Air is fed between the upper and lower left quadrants. The air flows downward into the lower left quadrant.
  • a negative pressure or vacuum is asserted by a low pressure compressor 105 such that gaseous permeation through the membrane 103a is facilitated. Since
  • the gases (such as nitrogen) that do not permeate through the membrane 103a, within the time allowed by the downward flow rate and length of the lower left quadrant 103ii, are exhausted out of the continuous membrane column 103 through discharge valve 103 b at the lower portion of the lower left quadrant 103ii.
  • the oxygen rich gases flow upwards, through outlet 104, and into low pressure recirculation pump 105.
  • the pressure of the oxygen rich gases at the outlet 104 is approximately 15 PSIA.
  • a low pressure recirculation pump 105 pumps the oxygen rich mainstream gases back up to approximately 25-40 PSIA.
  • a portion (e.g., 50%) of the recompressed gases are recirculated back into the continuous membrane column 103 into the upper left quadrant of the continuous membrane column 103.
  • O 2 continues to permeate the membrane 103 a from the oxygen rich gases in the upper left quadrant 103i into the upper right quadrant 103iv.
  • the remainder (e.g., 50%) of the oxygen rich gases are provided to a heat exchanger H.E.
  • Heat exchanger H.E. #1 which cools the gases from, for example, the range of approximately 200°F to 225°F to the range of approximately 100°F to 120°F.
  • Heat exchanger H.E. #1 and all of the other heat exchangers described hereinafter, may be configured as a series of parallel platelets (commonly called a "platelet heat exchanger") composed of, for example, copper. Although the size of the heat exchangers will depends on the power output of the system, platelet heat exchangers can be made small. Techniques for making such a heat exchanger are known and used in the aerospace industry.
  • Fig. 8A shows an exploded view of a platelet heat exchanger used in accordance with the principles of the present invention.
  • Fig. 8B shows the platelet heat exchanger of Fig. 8 A in an unexploded view.
  • Platelet heat exchanger 800 includes gas flow platelets 801, 803, and 805 interstacked with water flow platelets 802, 804, and 806.
  • the upper surface of each platelet 801-806 defines a channel of flow for the gas or water.
  • the upper surface may be patterned to define the channels using conventional photoetch processes.
  • As cooling water passes through the channels of a water flow platelet the water receives heat from the neighboring gas flow platelets and is converted to steam.
  • the cooled gases are provided to a high pressure compressor 106 where the gases are pumped to a high pressure of, for example, approximately 900 PSIA at a temperature of approximately 750°F.
  • These high pressure gases are provided to a heat exchanger H.E. #2 where they are cooled from, for ex-ample, approximately 750°F to approximately 100°F to 120°F.
  • the cool side of the heat exchanger H.E. #2 includes a water recirculation system.
  • the cooled high pressure gases then pass through a molecular sieve bed
  • the molecular sieve bed 107 extracts the H 2 O and CO 2 from the gases so that no ice or dry ice forms at the cryogenic portion of the oxygen production system. Only argon, nitrogen, carbon dioxide and oxygen exist in significant amounts at the outlet 108 of the molecular sieve bed 107.
  • the argon, nitrogen, carbon dioxide and oxygen mixture are provided to a heat exchanger H.E. #3 which cools the mixture from, for example, 100-120°F down to approximately -60°F.
  • This cool high pressure mixture is expanded through an expansion turbine 109 where the temperature of the mixture is reduced to a temperature below the freezing point of oxygen but above the freezing point of argon and nitrogen (e.g., -295°F).
  • the mechanical energy of the expansion turbine 109 is converted into electrical energy in generator 110, thereby improving the efficiency of the process.
  • the two phase mixture from expansion turbine 109 is provided to a distillation tower 111 where the liquid oxygen is separated from the gaseous argon and nitrogen.
  • the carbon dioxide, nitrogen and argon are either packaged for consumer use or may be exhausted into the environment. The impact of exhausting nitrogen and argon into the environment is negligible since argon and nitrogen are components of air and do not contribute to smog, the greenhouse effect, or acid rain. Furthermore, there are numerous commercial uses for carbon dioxide, nitrogen, and argon.
  • the liquid oxygen is provided to pump 112 where the liquid oxygen is pumped to a high pressure of, for example, approximately 3600 PSIA.
  • the work needed to pressurize the liquid oxygen is minimal (approximately 50 horsepower for a liquid oxygen flow of 3.4 pounds/second of liquid oxygen) compared to the work required to pressurize compressible gases.
  • Part of the liquid oxygen is stored in a liquid oxygen start tank 113 for starting up the system.
  • the high pressure oxygen is provided back to heat exchanger H.E. #3 where the high pressure oxygen is heated to, for example, approximately 50°F into the dense gaseous phase of oxygen. This heat for warming the oxygen is the heat lost from the argon, nitrogen, and oxygen mixture from the molecular sieve bed 107.
  • the warmed high pressure oxygen is passed through heat exchanger H.E. # 1 where the high pressure oxygen is heated to approximately 80°F to 100°F. This heat is taken from the low pressure oxygen, nitrogen, water, carbon dioxide, and argon mixture passing through heat exchanger H.E. 1 in the opposite direction from low pressure compressor 105.
  • the high pressure oxygen is thus prepared to be used with the gas generator 30 (Fig. 3).
  • oxygen is commercially available and need not be extracted from air on site. While the oxygen production system described above has many advantages, any source of high pressure oxygen may be used to provide oxygen to the gas generator 30 (Fig. 3). Furthermore, oxygen generation system 20 may generate high pressure oxygen for purposes other than for use in a combustion chamber.
  • GAS GENERATOR Fig. 3 shows gas generator 30 of Fig. 1. Oxygen gas passes through line
  • the oxygen gas is between 3400 and 3500 PSIA, between 60°F and 560°F, and at flow rate of approximately 3.4 lbm/s.
  • the other line 301 going to the mixing chamber 114 supplies high pressure steam.
  • the steam is at a pressure of between 3400 and 3500 PSIA, at a temperature between 560°F and 750°F, and at a flow rate of approximately 4.2 lbm/s.
  • the steam is mixed with the oxygen in the initial mixing chamber 114, which employs a series of baffles 302 to perform the mixing process.
  • the mixed gases have a pressure between 3400 and 3500 PSIA, a temperature between 510°F and 560°F, a flow rate of approximately 7.6 lbm/s, and mole percentages of 68.7 % H 2 O and 31.3% O 2 .
  • Table 1 illustrates inlet and outlet flow rates, temperatures, pressures, .and gas compositions at various stages of the exemplary embodiment industrial power generation system 1 as determined by simulation. Although Table 1 shows specific flow rates that correspond to a simulated 12.36 megawatt system. These flow rates may be scaled for other power outputs.
  • the mixed gases then go to a second mixing chamber 303 ("mixing unit 303") where fuel, such as methane gas, is added from a source of fuel 350 (Fig. 1).
  • fuel such as methane gas
  • methane gas is added at a pressure between 3400 and 3500 PSIA, at a temperature of approximately 80°F, and at a flow rate of approximately 0.5 lbm/s.
  • This chamber 303 (Station 4) contains conventional high temperature Raschig rings 304 to promote turbulence and mixing of the fuel, oxidizer and steam to produce a very uniform mixture at the injector inlet chamber 307.
  • a control valve 305 is located between the mixing chamber 303 and the injector inlet chamber 307 at Station 5.
  • Control valve 305 is spring loaded to control the amount of flow entering the combustion chamber 118. Control valve 305 also serves as an emergency shut down should something happen downstream that might result in a rapid increase or reduction in chamber pressure.
  • a fuel supply valve 303a supplying fuel to mixing chamber 303 is automatically closed while a nitrogen purge value 303b supplying nitrogen to mixing chamber 303 is opened.
  • a second purpose of the nitrogen purge is to assist in starting up the unit by cooling the mainstream gases until the diluent steam system is fully operational.
  • the mixture of fuel, oxidizer and steam is introduced into the combustion chamber 118 through a series of small circular injection ports 309 provided in an injector plate 116.
  • Injector plate may be composed of, for example, stainless steel.
  • the mixture has at flow rate of 8.1 lbm/s and mole percentages of 62.9% H 2 0, 28.7% O 2 and 8.4% CH 4 .
  • ports 309 can be sized to provide adequate injection velocity so as to prevent back flash into the upstream injection.
  • the ports 309 should be sized so that the injection velocity of the mixed gases is greater than the flame propagation velocity.
  • the dimensions of ports 309 will depend on the mixture composition and temperature desired and can be empirically determined.
  • combustion chamber 118 The pre-mixing of the oxygen, fuel, .and ste.am prior to injection into combustion chamber 118 assures complete combustion of the gases in the combustion chamber 118, thereby improving the combustion efficiency.
  • An ignition plug 117 (“igniter 117"), at Station 6, is placed at the center of the injection plate 116, in one embodiment, and is used to initiate the combustion process.
  • the walls of combustion chamber 118 are cooled by water passing through a series of platelets 308 that make up the chamber wall. This form of cooling, known as transpiration cooling, cools the walls of the chamber 118 to a temperature (e.g., 700°F to 900°F) well below the melting point of the material
  • transpiration cooling has only a negligible cooling effect on the mainstream gases.
  • Fig. 6A is an exploded isometric view of two flat ring-shaped platelets 610 and 620 which are part of the series of platelets 308.
  • Platelets 610 and 620 may be composed of, for example, stainless steel. Platelets 610, 620 and all the other platelets of the series of platelets 308 are stacked together. Grooves are formed in at least one of the facing surfaces to allow water to pass along the grooves and cool the platelets such as platelets 610 and 620.
  • the stack of platelets 308 forms the wall of combustion chamber 118.
  • Fig. 6B is a detailed exploded isometric view of portion 6B of Fig. 6A.
  • Fig. 6B shows that each platelet 610 and 620 has a grooved surface 622 with open channels 624 formed therein by, for example, etching.
  • the open channels 624 run from the outer diameter to the inner diameter.
  • Platelets 610 and 620 may be, for example, 0.010 inches thick and have ridges having a cross section of, for example, 0.005 wide by 0.005 deep. Platelets 610 and 620 are stacked together such that facing surfaces of adjacent platelets are in physical contact thereby forming channels 624 of platelet 610.
  • the other platelets of the series of platelets 308 have similar channels.
  • the initial combustion may take place in an oxidizer rich atmosphere, which means there is more oxygen present in the mixture than is required to burn all the fuel introduced into the initial combustion process.
  • the combustion gases from chamber 118 are at 3200°F and 3300 PSIA and include mole percentages of 79.3% H 2 0, 11.7% O 2 , 8.4% CO 2 , and 0.6% OH with traces of CO.
  • these combustion gasses require further cooling down prior to entering the turbines which contain iron or steel. Alternatively, cooling down may not be required if ceramic materials are used in the turbines immediately downstream from chamber 118.
  • An extension 320 is added to the initial chamber 118 where coolant water is injected from injectors 120a and 120b and mixed with the mainstream gases at Station 8.
  • coolant water is injected at approximately 3300 PSIA, 150°F, and 0.35 lbm/s.
  • This water injection provides some initial temperature reduction (e.g., down to approximately 3000°F in the exemplary embodiment) in the combustion gases to make the gas temperature compatible with the materials (e.g., copper in the exemplary embodiment) used in heat exchanger H.E. #4.
  • copper has a melting point below the temperature (e.g., 3000°F) of the hot gases provided to heating exchanger H.E.
  • the copper remains structurally sound because the copper platelets are being continuously cooled by the cool water provided to the cold side of the heat exchanger H.E. #4.
  • the coolant water is injected into a cooling reservoir 321 provided within the walls of extension 320 which cools the walls of the extension 320 to well below the melting point of the materials (e.g., steel) that make up the walls of extension 320.
  • the walls of extension 320 remain structurally sound even if the mainstream gases are at a temperature above the melting point of the material (e.g., steel) making up the walls of the extension 320.
  • a solid concave disc 119 (i.e., splash plate 119 made of, for example, copper) is placed in the center of the mainstre.am gases to catch the H 2 O rich gases just downstream of the injection ports 120a and 120b.
  • these H 2 O rich gases are at approximately 3300 PSIA, 3000°F, and 8.45 lbm/s with mole percentages of 80.3% H 2 0, 11.1% O 2 , 7.9% CO 2 , 0.6% OH and traces of CO.
  • Splash plate 119 is kept from melting due to the cooling effect of the cooling water splashing on its surface.
  • splash plate 119 Due to its concave shape, splash plate 119 throws the H 2 O rich gases outwards around the ends of the splash plate 119 to assist in thoroughly mixing the injected H 2 O with the other mainstream gases.
  • the water injection system and splash plate 119 lower the temperature of the mainstream gases while adding more mass flow for driving the downstream turbines.
  • splash plate 119 has mixing efficiency advantages, other in line mixing structures may be used. A mixing structure may even be completely omitted with some possible sacrifice in mixing efficiency.
  • Two ways to increase turbine output power are to increase turbine inlet gas temperatures and/or increase the mass flow to the turbine stages. Inlet gas temperature is limited by the materials used in the turbines such as steel.
  • Adding water increases the mass flow and lowers the gas temperature making this a very acceptable trade off in the overall power output of the turbine stages. This is particularly significant in that the molecular weight of the steam is less than that of the mainstream gases and a low molecular weight gas will produce more horsepower per unit mass than a high molecular weight gas.
  • the temperature of the mainstream gases is reduced incrementally over the length of the gas generator. In the heat exchanger H.E. #4, the temperature of the mainstream gases is lowered again to an intermediate temperature prior to entering the turbines. In the exemplary embodiment, this intermediate temperature is approximately 2110°F. Cooling water is provided to the cold side of heat exchanger H.E. #4.
  • this cooling water is provided at a temperature of approximately 80°F and 4.2 lbm/s.
  • this cooling water is heated up to steam (e.g., at approximately 750°F).
  • This steam is mixed with oxygen in mixing chamber 114 (Fig. 3).
  • the heat lost by the mainstream gases in heating this steam is not lost in the overall system.
  • the temperature of the mainstream gases is lowered further to approach the temperatures that can be handled by the turbines of primary turbine stage 126
  • these mainstream gases are at approximately 3100 PSIA and the temperature is lowered to approximately 2110°F.
  • the region downstream of the heat exchanger H.E. #4 has an additional water injection Station 9 having injectors 122a and 122b (Fig. 3).
  • the additional water injection station is used to control the input temperature to the primary turbine stage 126 to design conditions within ⁇ 10°F by sensing the inlet temperature to the primary turbine stage 126 (Fig. 4), Station 10, and controlling the amount of water injected at injectors 122a and 122b based on the temperature measurement.
  • the desired inlet temperature for primary turbine stage 126 is set, in the exemplary embodiment, for 2000°F.
  • the amount of water injected is increased when the temperature climbs above 2000°F and is decreased when the temperature falls below 2000°F.
  • a splash plate 121 (Fig. 3), which may be similar to splash plate 119, is positioned just downstream of injectors 122a and 122b, and is employed to mix the water with the mainstream gases from extension 320 prior to exiting the gas generator 30.
  • Natural gas may contain significant quantities of hydrogen sulfide which, when heated in an oxygen rich environment, forms sulfur dioxide. This sulfur dioxide, if emitted into the environment, contributes to acid rain.
  • the sulfur dioxide byproduct may be eliminated by injecting calcium rich lime water through or near the injectors 122a and 122b.
  • the calcium of the lime water combines with the sulfur in the natural gas to form calcium sulfate, a byproduct which does not contribute to acid rain, the greenhouse effect, or smog.
  • the calcium sulfate passes with the mainstream gases and accumulates in the storage tank 154 with water.
  • water As water is a byproduct of the combustion process, water (with calcium sulfate) is drained from storage tank 154 to prevent water overflow in the condenser/collector 148. Thus the calcium sulfate is drawn from the industrial power generation system 1.
  • the sulfur dioxide byproduct can also be eliminated using conventional sulfur filtering of the natural gas prior to introduction into the gas generator 30.
  • Output mainstream gases of the gas generator 30 then go to the main power system 40 (Fig. 4) where the potential energy in the gas stream is converted into mechanical energy in the turbine stages 126, 132, 134, and 136 and then into electrical energy in the generators 128 and 137.
  • these output mainstream gases are at approximately 3100 PSIA, 2000°F, and 8.69 lbm/s having a mole percentage of 81.0% H 2 0, 10.8% O 2 , 7.7% CO 2 , 0.5% OH.
  • a 0.5% mole percentage of OH and minute traces of CO are approximated in the simulation, OH and CO will, in practice, be combusted in the gas generator 30 leaving only H 2 O, O 2 , .and CO 2 ..
  • a conventional infrared sensor at the outlet of gas generator 30 can detect the molecules OH .and CO .and use a conventional feedback mechanism to add more oxygen to gas generator 30 so that all OH and CO molecules are completely combusted within gas generator 30.
  • a similar feedback system can be provided at each reheater 133 and 135 to ensure that enough oxygen is introduced to completely combust the fuel.
  • the gas generator 30 (Fig. 3) may be made very small.
  • gas generator 30 need only have an outside diameter of approximately 12 inches, an inside diameter of approximately 8 inches, and a length of approximately 8 feet.
  • the main power system 40 for generating electrical power is shown in Figure 4.
  • the hot high pressure mainstream gases exiting gas generator 30 expand within a primary (first stage) turbine stage 126 (or "radial inflow turbine 126") to produce mechanical energy.
  • radial inflow turbine 126 receives 2503 horsepower of energy from the mainstream gases.
  • This mechanical energy (“brake horsepower") of turbine stage 126 is converted to electrical energy in electrical generator 128.
  • the electrical generator 128 efficiency is approximately 98.5 % and thus the electrical energy produced by the 2503 horsepower is 1.84 megawatts (2503 hp * (746 watts
  • the mainstream gases exiting radial inflow turbine 126 are at approximately 1000 PSIA and 1585°F.
  • Primary turbine stage 126 may be a single stage radial inflow turbine that operates at approximately a 3/1 pressure ratio with a design inlet temperature (e.g., 2000°F) and pressure (approximately 3100 PSIA).
  • the high inlet pressure allows for a very compact turbine 126.
  • the combination of flow and pressure ratio (3/1) is such that this turbine operates in the specific speed range for radial inflow turbines, so that a relatively high efficiency can be expected.
  • a radial inflow turbine runs smoothly and is relatively uninfluenced by minor fluctuations in inlet flow. Thus, it will drive generator 128 stably and smoothly.
  • Reheater 131 is introduced between the radial inflow turbine 126 and the high pressure secondary turbine stage 132 (or "axial turbine stage 132").
  • An embodiment of reheater 131 is shown in Fig. 7.
  • Reheater 131 may be composed of a single hollow tube 600 made of, for example, stainless steel, copper or other material of high heat transfer coefficient, which is bent to form a solinoidal shape having an inlet 601, solinoidal middle portion 603 and an outlet 602. Reheater 131 receives fuel at inlet 601. The fuel travels through hollow tube 600 and is combined with fuel at fuel inlet 604. In the exemplary embodiment, this fuel is methane at approximately 1000 PSIA, 80°F, and 0.081 lbm/s.
  • the mainstream gases e.g., at a temperature of approximately 1585°F
  • the ignition temperature of the fuel e.g., methane
  • the fuel will spontaneously ignite in the presence of the oxidizer rich mainstream gases and the hollow tube 600 will not melt.
  • the bends in the middle portion 603 cause mixing, and thus efficient combustion, of the fuel and mainstream gases.
  • the outlet 602 is made sufficiently far from the inlet 601 in terms of mainstream gas running distance such that complete combustion occurs prior to entering the next turbine stage 132.
  • the temperature of the mainstream gas exhausted from turbine 126 is not enough to spontaneously ignite the fuel in which case .an ingiter is, of course, necessary in reheater 131.
  • This combustion of the fuel/mainstream gas mixture in reheater 131 heats the mainstream gases exiting reheater 131 to bring the mainstream gas temperature at the inlet to the axial turbine stage 132 to design conditions.
  • the fuel/mainstream gas mixture entering reheater 131 is at approximately 1000 PSIA, 1560°F, and 8.771 lbm/s having mole percentages of 80.0% H 2 0, 10.6% O 2 , 1.2%
  • the mainstream gases exiting reheater 131 are at approximately 1000 PSIA, 2000°F, and have mole percentages of 82.8%) H 2 O, 8.3% oxygen, 8.9% carbon dioxide, and minute traces of HO and CO.
  • the amount of fuel needed to increase the temperature to design conditions e.g., 2000°F is so small weightwise, that the performance of the secondary turbine stages 132, 134 and 136 is enhanced very efficiently.
  • a fairly small amount of fuel (e.g., methane at 0.081 pounds/second) is required to raise the mainstream gas temperature back up to inlet temperature design conditions for turbine stage 132.
  • additional reheaters 133 and 135 are provided before turbine stages 134 and 136, respectively. Raising the turbine output temperature by 500°F will produce a 23% increase in horsepower for the next stage assuming identical pressure ratios across the stages. Again this is a cumulative effect in that successive stages 134 and 136 are influenced by the heat addition in the initial reheater stage 131 tending to make the entire process more efficient.
  • the reheaters 131, 133 and 135 are made up of conventional spiral tube shaped mixers.
  • the inside diameter of the tube may be approximately five inches for a 12.36 megawatt system but may be scaled according to the power output.
  • the mainstream gases and the added fuel are forced through the hollow coiled tubes, the mainstream gases experience shear which swirls and mixes the combusting gaseous mixture as the mixture proceeds through the reaction chamber.
  • the spiral tubes are made long enough that the mainstream gases have sufficient residence time for the fuel to completely burn.
  • the stay time, and thus the length of the tubes, is a function of the flow rate, combustion temperature, and can be conventionally determined.
  • Each of the secondary turbine stages 132, 134 and 136 may consist of three axial turbines in series as the pressure ratio across an individual axial turbine should be approximately 1.6/1 or less for good turbine efficiency.
  • Pressure ratio is defined as inlet pressure over the discharge pressure for a specific turbine or turbine stage.
  • the inlet pressure to the high pressure secondary turbine stage 132 is approximately 1000 PSIA and the discharge pressure is approximately 245 PSIA resulting in an approximately 4/1 pressure ratio.
  • the temperature of the mainstream gases is reduced from approximately 2000°F to 1475°F across turbine stage 132.
  • Three axial turbines in series would be used to make up the turbine stage 132.
  • the mainstream gases from reheater 131 expand within turbine stage 132 to produce mechanical energy in turbine stage 132 which is converted to electrical energy in generator 137.
  • the mainstream gases at 1000 PSIA and 2000°F expand down to 245 PSIA and 1475°F within turbine stage 132 to produce 3209 horsepower of mechanical energy which is converted to 2.36 megawatts of electrical power assuming a turbine stage 132 efficiency of 98.5%. This 2.36 megawatts represents 18.8% of the total output power of 12.56 megawatts.
  • the mainstream gases which exit this turbine stage 132 go to the second reheater 133 of the same design as reheater 131, where the mainstream gas temperature is raised back up to the design inlet temperature of turbine stage 134 by injecting more fuel into the mainstream gases.
  • the temperature of the 245 PSIA mainstream gases is raised to approximately 2000°F by adding approximately 0.115 lbm/s of CH 4 .
  • the fuel/mainstream gas mixture has a flow of 8.886 lbm/s and mole percentages of 81.4% H 2 O, 8.1% O 2 , 1.7% CH 4 , 8.7% CO 2 , and traces of OH and CO.
  • the mainstream gases After combustion, the mainstream gases have mole percentages of 84.9% H 2 O, 4.7% O 2 , 10.4% CO 2 and traces of OH and CO.
  • the mainstream gases from reheater 133 expand within the second turbine stage ("intermediate pressure secondary turbine stage 134") to produce mechanical energy in turbine stage 134 which is converted to electrical energy in generator
  • the mainstream gases at 245 PSIA and 2000°F expand down to 60 PSIA and 1340°F within turbine stage 134 which may contain three axial turbines in series. This expansion produces approximately 3270 horsepower of mechanical energy which is converted to 2.40 megawatts of electrical power assuming a turbine stage 134 efficiency of 98.5%. This 2.40 megawatts represents 19.1% of the total output power of 12.56 megawatts.
  • the mainstream gases which exit this turbine stage 134 go to the third reheater 135 of the same design as reheater 131, where the mainstream gas temperature is raised back up to the design inlet temperature of turbine stage 136 by injecting more fuel into the mainstream gases.
  • the temperature of the 60 PSIA mainstream gases is raised to approximately 2000°F by adding approximately 0.118 lbm/s of CH 4 .
  • the fuel/mainstream gas mixture has a flow of 9.004 lbm/s and mole percentages of 83.4% H 2 O, 4.6% O 2 , 1.7% CH 4 , 10.3% CO 2 , and traces of OH and CO. After combustion, the mainstream gases have mole percentages of 86.9%)
  • the mainstream gases from reheater 135 expand within the third turbine stage ("low pressure secondary turbine stage 136") to produce mechanical energy in turbine stage 136 which is converted to electrical energy in generator 137.
  • the mainstream gases at 60 PSIA and 2000°F expand down to 20 PSIA and 1590°F within turbine stage 134 (which typically contains three axial turbines in series). This expansion produces approximately 2678 horsepower of mechanical energy which is converted to 1.97 megawatts of electrical power assuming a turbine stage 134 efficiency of 98.5%. This 1.97 megawatts represents 15.7% of the total output power of 12.56 megawatts.
  • the mainstream gases After exiting turbine stage 136, the mainstream gases now enter a post treatment phase, where heat is extracted from the mainstream gases and utilized in an auxiliary power system 50 (Figs. 1 and 5) for further electrical power generation.
  • the auxiliary power system 50 (Fig. 5) includes an auxiliary fluid circuit (e.g., a water/steam circuit) and is shown in Figure 5.
  • the exhaust gases from turbine stage 136 in main power system 40 have very little potential energy, as the pressure has been reduced to 20 PSIA in the exempl-ary embodiment. However, the exhaust gases still possess considerable thermal energy even after passing through turbine stages 126, 132, 134 and 136 because of the reheating in reheaters 131, 133 .and 135.
  • the mainstream gas exiting turbine stage 136 is approximately 1590°F.
  • the thermal energy content of the mainstream gas is further enhanced by the fact that approximately 86.9% of the mainstream gas is steam which when condensed as water provides a significant heat source for the auxiliary steam power system 50.
  • Post treatment of the power system's effluent consists of taking mainstream gases from mainstream power system 40 through a heat exchanger H.E. #5 to reduce the gas temperature.
  • the 20 PSIA mainstream gases are cooled from 1590°F to 230°F which results in a heat loss rate of 19,710,000 Btu/hr from the mainstream gases.
  • This cooled effluent then passes through a heat exchanger H.E. #6 in which the steam of the mainstream gas is condensed into water.
  • this condensation and cooling results in a heat loss of approximately 23,900,000 Btu/hr for a total heat loss in heat exchangers H.E. #5 and H.E. #6 of 43,610,000 Btu/hr.
  • the effluent from main power system 40 having mole percentages of 86.9% H 2 O, 1.1% O 2 , 12.0% CO 2 and traces of OH and CO, results in a cooled effluent containing only H 2 O, CO 2 , and O 2 .
  • Other element mole percentages are negligible.
  • the two-phase mixture e.g., only H 2 O is in the liquid phase
  • the heat exchanger H.E. #6 goes to a scrubber 148 (Fig. 1).
  • the excess water from the scrubber 148 (Fig. 1) is sent to storage 154 (Figs.
  • H 2 O pump 151 that raises the water pressure to approximately 3500 PSIA.
  • the high pressure water from pump 151 passes through heat exchanger H.E. #7 to raise the temperature to approximately 200°F prior to returning to injectors 120a and 120b in the gas generator 30.
  • H 2 O from an auxiliary flow circuit 502 is heated to the turbine inlet temperature (e.g., 1200 °F) of auxiliary steam turbine stage 142 by the turbine exhaust effluent from the primary power generation system 40 passing through heat exchangers H.E. #5 and #6.
  • the evaporator side of the second exchanger H.E. #6 has water entering, for example, at approximately 150°F pumped to a pressure of, for example, approximately 1000 PSIA by H 2 O pump 152.
  • the output from exch-anger H.E. #6 is low temperature steam which is delivered to an exchanger H.E. #5 that superheats the steam to, for example, a temperature of approximately 1200°F at a pressure of approximately a 1000 PSIA.
  • the 43,610,000 Btu/hr of heat from the mainstream gases exhausted from main power system 40 is transferred to the steam of the auxiliary power system 40.
  • the performance of evaporation and condensation in two separate heat exchanges is a very efficient means of transferring heat.
  • the surface area required for latent heat transfer in heat exchanger H.E. #6 is much smaller than the surface area needed for sensible heat transfer in H.E. #5 even though the total latent heat transferred in heat exchanger H.E. #6 is greater than the sensible heat transferred in heat exchanger H.E. #5.
  • auxiliary turbine stage 142 which converts a percentage of the heat transferred to the steam in heat exchangers H.E. #5 and H.E. #6 into mechanical energy.
  • the auxiliary turbine stage converts 13,900,000 Btu/hr of the 43,610,000 Btu/hr of heat received by the steam in heat exchangers H.E. #5 and H.E. #6 into 5459 horsepower assuming a turbine stage 142 efficiency of 31.87%.
  • This 5459 horsepower of the auxiliary turbine stage 142 efficiency is converted into 4.01 megawatts of electrical power in generator 137 assuming a generator efficiency of 98.5%.
  • This 4.01 megawatts represents 31.4% efficiency for auxiliary turbine stage 142 together with generator 137 and represents 31.92% of the total output power of 12.56 megawatts.
  • Auxiliary turbine stage 142 may be two radial inflow turbines in series, which power either the main electrical power generator 137 or a separate generator system that stands alone. Effluent from the auxiliary turbine stage 142 is steam at, for example, a temperature of approximately 230°F and a pressure of approximately 10 PSIA. The steam is then condensed to water in heat exchanger H.E. #1 and returned to heat exchangers H.E. #5 and #6 by H 2 O pump 152.
  • the power generation system of the present invention offers the highest efficiencies available anywhere at this time, emits essentially zero pollution, and is very compact.
  • Oxygen and fuel e.g., methane or natural gas
  • the system is more compact than conventional systems because the gas generators and high pressure turbines can be made smaller for a given power output due to the high pressure operation.
  • the industrial power generation system 1 (Fig. 1) can be made approximately 30% smaller (for a 12.56 megawatt output) than the conventional industrial power generation systems of equivalent power output.
  • Elimination of the nitrogen from the combustion process means that substantially no smog is produced by this power generation system.
  • Combination of the sulfur with the calcium of the injected lime water means that substantially no acid rain is ever caused by this power generation system.
  • the gas temperatures in the combustion chamber 118 are as high as they can get (e.g., over 6000°F).
  • the chamber walls cannot typically handle this high temperature.
  • water/steam is added to the combustion process to keep the combustion temperature low enough (e.g., 3200°F) to not damage the combustion chamber 118.
  • the premixed gases from the injector cavity are transmitted through the injector plate 116 through a series of injector ports 309 uniformly distributed across the injector plate 116.
  • An igniter 117 e.g., an ignition plug
  • Combustion takes place at a high pressure such as approximately 3300 PSIA. This high pressure has not previously been used in the power industry. Of course, other appropriate high pressures may also be used.
  • the combustion chamber 118 in the power generation system 1 of the present invention is cooled using, for example, transpiration cooling with water/steam injected through the wall similar to that employed in a liquid rocket engine.
  • Photo-etched, annular shaped, stainless steel wafers 610 and 620 (Figs 6A and 6B) containing minute channels 624 are used to distribute the coolant through the wall to maintain a reasonably cool temperature (e.g., approximately 800°F to 900°F) for the wall of combustion chamber 118.
  • Additional water is injected at injectors 120a and 120b and mixed into the mainstream just downstream of the main combustion chamber 118.
  • the heat exchanger H.E. #4 extracts heat from the mainstream gases and inputs heat into the steam being delivered to the premix chamber 114 (i.e., "mixer 114").
  • the high temperature of the steam in the premix chamber 114 promotes mixing of the steam with the oxygen.
  • the reaction time in the combustion chamber 118 9 is reduced allowing combustion to take place almost instantaneously.
  • Second water injectors 122a and 122b and splash plate 121 are located just downstream of the heat exchanger H.E. #4.
  • the amount of water injected at this station is controlled by a thermocouple ("temperature sensor 180" in Fig. 1) at the inlet of the primary turbine stage 126.
  • the inlet temperature to turbine stage 126 is set at a prescribed design condition and the amount of water injected in extension 320 is controlled to maintain this condition plus or minus ten degrees Fahrenheit.
  • a radial flow inlet turbine (i.e., turbine stage 126) serves as the first phase of the main power generation system 40.
  • a radial inflow turbine was selected because the high inlet pressure (approximately 3000 PSIA) and relatively low speed (3600 RPM) require a low specific speed turbine for reasonable operating efficiency and compact sizing. Axial turbines perform better at high specific speeds while radial inflow turbines perform well at low specific speeds.
  • Reheater 131 (Fig. 4) is installed between the primary turbine stage 126 and the high pressure secondary turbine stage 132 to heat the mainstream gases prior to entering to entering turbine stage 132.
  • Another reheater 133 is provided downstream of turbine stage 132 to reheat the mainstream gases prior entering the intermediate pressure turbine stage 134.
  • This stage 134 is followed by a third reheater 135 where the fuel added is almost enough to use up the excess oxygen from the original combustion mixture. Therefore the exhaust gas from this reheater 135 will have trace amounts of unburned hydrocarbons and only a small amount of oxygen at the design inlet temperature for the next turbine stage 136.
  • the combined effect of the reheaters 131, 133 and 135 on the overall power generated is a 10% increase after the high pressure secondary turbine stage 132, a 27% increase after the intermediate pressure secondary turbine stage 134, and a 42% increase after the low pressure secondary turbine stage 136 (all compared to the power generated by just the primary turbine stage 126).
  • These results illustrate the cumulative effect of the reheaters which increase the overall power output of the main power system 40 by a substantial margin.
  • the turbine stages 126, 132, 134 and 136 most of the pressure in the mainstream gases has been dissipated in driving turbines. However, the mainstream gases are still relatively hot.
  • Auxiliary steam turbine stage 142 makes system 1 (Fig. 1) a combined cycle system.
  • the heat from the mainstream gas exiting the turbine stage 136 is transferred to an auxiliary stream of steam in heat exchangers H.E. #5 and #6.
  • the resulting steam is then sent to steam turbine 142 for additional power generation.
  • the steam turbine 142 is part of a closed loop system where the steam used to drive steam turbine 142 is cooled and condensed in heat exchanger H.E. #7 by the water recycled to the combustion chamber 118.
  • the water is evaporated and superheated by the primary gas stream exhausted from main power system 40.
  • the reheaters 131, 133 and 135 from the main power system 40 increase the amount of energy that can be retrieved by and used in the auxiliary steam turbine 142.
  • the auxiliary power system 50 accounts for approximately 30% of total power output of system 1.
  • the effluent from main power system 40 has mostly H 2 O in the liquid phase and CO 2 in the gaseous phase.
  • This effluent empties into a separator tank 148 where the water is drained off. Most of the water is sent back to the gas generator 30 through pump 151 and heat exchanger H.E. #7, some is used for make-up in the auxiliary steam power system 50 and the remainder becomes a worthwhile product for use as needed.
  • Gas from the separator 148 is primarily CO 2 with some O 2 (if O 2 was oversupplied from the oxygen generation system 20) The CO 2 and O 2 , may be separated and sold commercially or used as useful products.
  • the amount of oxygen supplied by oxygen production system 20 is lowered so that there is no extra O 2 left in the effluent. In that case, only CO 2 is present in the gaseous phase in separator 148.
  • the system is a substantially closed loop system where relatively little, if any, pollution is returned to contaminate the environment.
  • the system of the present invention can be adapted to modify an existing gas generator power plant using existing turbines, generators, pumps, and any gas separating equipment.
  • Existing technology for making oxygen from air would be incorporated in the plant as well as an existing steam power generation package.
  • Nitrogen and argon recovery would come from existing oxygen production systems, as would carbon dioxide recovery. Only the mixing chambers, the combustion chamber, heat exchangers, and reheaters would necessarily have to be fabricated to suit the modified process.
  • the oxygen is combined with fuel at a stoichiometric ratio before combustion in chamber 118.
  • Oxygen is then supplied separately to the reheaters 131, 133 and 135 because there is no excess oxygen at the outlet of the gas generator 30.
  • the quantity of oxygen and fuel input to the reheaters 131, 133 and 135 depends on how much unburned fuel or excess oxygen is present at the outlet of gas generator 30.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

L'invention concerne un générateur de gaz peu polluant qui comporte une source d'un mélange de gaz riche en oxygène et de carburant, le gaz riche en oxygène comportant moins d'azote que l'air et plus d'oxygène que l'air. Le mélange est introduit dans une chambre de combustion où il est mis à feu. Le mélange préalable de l'oxygène et du carburant avant son introduction dans la chambre de combustion permet d'obtenir une combustion plus efficace. On utilise de l'eau comme agent d'absorption de chaleur. Les gaz du flux principal provenant de la chambre de combustion se détendent dans une turbine primaire, et sont ensuite chauffés à nouveau avant de se détendre dans une turbine secondaire. La chaleur provenant des gaz du flux principal est transférée vers un écoulement auxiliaire d'eau qui se transforme en vapeur et se détend dans une turbine auxiliaire. Le système de la présente invention permet d'obtenir des rendements égaux, voire supérieurs à 65 %. En outre, le système produit peu ou pas de pollution, et est compact par rapport à des systèmes de production industrielle d'énergie de puissance similaire.
PCT/US1998/022763 1997-10-28 1998-10-27 Systeme de production industrielle d'energie a rendement eleve, non polluant et de technologie de pointe WO1999022127A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
AU12023/99A AU1202399A (en) 1997-10-28 1998-10-27 An advanced technology pollution free, highly efficient industrial power generation system
EP98955147A EP1029167A1 (fr) 1997-10-28 1998-10-27 Systeme de production industrielle d'energie a rendement eleve, non polluant et de technologie de pointe
CA002306710A CA2306710A1 (fr) 1997-10-28 1998-10-27 Systeme de production industrielle d'energie a rendement eleve, non polluant et de technologie de pointe
JP2000518198A JP2003526035A (ja) 1997-10-28 1998-10-27 進歩的技術の、汚染物フリーで高効率な産業発電システム

Applications Claiming Priority (4)

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US6340597P 1997-10-28 1997-10-28
US60/063,405 1997-10-28
US17836498A 1998-10-23 1998-10-23
US09/178,364 1998-10-23

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US6910335B2 (en) 2000-05-12 2005-06-28 Clean Energy Systems, Inc. Semi-closed Brayton cycle gas turbine power systems
WO2010104547A3 (fr) * 2009-03-09 2010-11-04 Clean Energy Systems, Inc. Procédé et système pour améliorer une sortie de puissances de centrales électriques à cycle thermique renouvelable
EP2706211A1 (fr) * 2012-09-10 2014-03-12 Siemens Aktiengesellschaft Installation de turbine à gaz avec installation de postcombustion pour la séparation du CO2
EP2759689A1 (fr) * 2013-01-28 2014-07-30 Alstom Technology Ltd Système d'alimentation électrique d'urgence comprenant une pile à combustible alimentée en hydrogène
US8810126B2 (en) 2007-12-26 2014-08-19 Olympus Corporation Light source device and endoscope apparatus comprising the same
CN110030047A (zh) * 2019-05-21 2019-07-19 福建省东锅节能科技有限公司 三次再热发电系统及其工作方法

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US7556670B2 (en) * 2006-03-16 2009-07-07 Aylsworth Alonzo C Method and system of coordinating an intensifier and sieve beds
JP5698780B2 (ja) * 2013-03-18 2015-04-08 オリンパス株式会社 光源装置およびそれを備えた内視鏡装置

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US6910335B2 (en) 2000-05-12 2005-06-28 Clean Energy Systems, Inc. Semi-closed Brayton cycle gas turbine power systems
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US9587791B2 (en) 2007-12-26 2017-03-07 Olympus Corporation Light source device and endoscope apparatus comprising the same
US10801677B2 (en) 2007-12-26 2020-10-13 Olympus Corporation Light source device and endoscope apparatus comprising the same
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EP2706211A1 (fr) * 2012-09-10 2014-03-12 Siemens Aktiengesellschaft Installation de turbine à gaz avec installation de postcombustion pour la séparation du CO2
EP2759689A1 (fr) * 2013-01-28 2014-07-30 Alstom Technology Ltd Système d'alimentation électrique d'urgence comprenant une pile à combustible alimentée en hydrogène
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CN110030047A (zh) * 2019-05-21 2019-07-19 福建省东锅节能科技有限公司 三次再热发电系统及其工作方法

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CA2306710A1 (fr) 1999-05-06
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JP2003526035A (ja) 2003-09-02

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